Process of reforming a gasoline with an alumina-platinum-halogen catalyst



Patented Aug. 16, 1949 PROCESS OF REFORMING A GASOLINE WITH AN ALUMINA-PLATINUM-HALO- GEN CATALYST Vladimir Haensel, Clarendon Hills, 111., amino: to Universal Oil Products Company, Chicago, 111., a corporation of Delaware No Drawing. Application November 28, 1947,

' Serial No. 788,673

This invention relates to a reforming process and more particularly to a process for the reforming of a saturated gasoline fraction in the presence of a particular catalyst and under selected conditions of operation.

The saturated gasoline fraction to be treated in accordance with the present invention comprises straight run gasoline, natural gasoline, etc. The gasoline fraction may be a full boiling range gasoline having an initial boiling point within the range of about 50 to about 100 F. and an end boiling point within the range of about 375 to about 425 F., or it may be a selected fraction thereof which usually will be a higher boiling fraction, commonly referred to as naphtha, and generally having an initial boiling point of from about 150 to about 250 F. and an end boiling point within the range of about 350 to about- The term reforming is well known in the petroleum industry and refers to the treatment of gasoline fractions to improve the antiknock characteristics. Straight run gasolines contain naphthenic hydrocarbons, particularly cyclohexane compounds, and paraflinic hydrocarbons which usually are of straight chain or slightly branched chain structure, as well as varying Proportions of aromatic hydrocarbons. In order to obtain best results in reforming operations it is desired to dehydrogenate the naphthenic hydrocarbons to produce aromatics, to cyclicize the straight chain paraffinic hydrocarbons to form aromatics, as well as to effect a controlled type of cracking which is selective both in quality and in quantity. In addition various other concomitant reactions occur such as isomerization, hydrogen transfer, etc.

The cracking or splitting of carbon to carbon bonds is one of the important factors in a successful reforming process. Controlled or selective cracking is highly desirable since such cracking will result in a product of improved antiknock characteristics. In general, the lower molecular weight products have higher octane numbers,

and thus a final gasoline product of lower average molecular weight will usually have a higher octane rating. Further. during the cracking reaction. isomerization or other molecular rearrangement occurs which also results in products momma (01.198-50) 2 However. the cracking must be selective and must not result in the decomposition of the normally liquid hydrocarbons substantially or completely into normally gaseous hydrocarbons. The desired selective cracking generally comprises the splitting of a higher boiling hydrocarbon molecule into two molecules both of which are normally liquid hydrocarbons. To a lesser extent it comprises the removal of methyl, ethyl and, to a still lesser extent, propyl groups, in the form of methane, ethane and propane, However, the removal of these radicals is controlled so that not more than one or possibly two of such radicals are removed from a given molecule. For example, decane may be reduced to two pentane molecules, heptane to hexane, nonane to octane or heptane, etc. On the other hand uncontrolled or nonselective cracking will result in the decomposition of normally liquid hydrocarbons into normally gaseous hydrocarbons as, for example, by the continued demethylation of normal heptane to produce 7 molecules of methane.

Another important objection to non-selective or uncontrolled cracking is that this type of cracking will result in the more rapid formation of larger quantities of coke or carbonaceous material which deposits on the catalyst and decreases or destroys its activity to catalyze the desired reactions. This in turn results in shorter processing cycles or periods, with the necessity of more frequent regeneration of the catalyst by burning the carbonaceous products therefrom or,

should the catalyst activity be destroyed, it will be necessary to shut down the unit to remove the old catalyst and replace it with new catalyst.

Another important feature in successful reforming processes is the matter of hydrogen production and consumption. Investigation has shown that the presence of hydrogen in the reforming zone further tends to decrease the amount of carbonaceous deposits on the catalyst. Reforming processes effected in the presence of hydrogen are known as Hydroforming." In view of the fact that the cost of hydrogen is quite high, it is essential that there be no net consumption of hydrogen or, in other words, at least as much hydrogen must be produced in the process as is consumed therein.

In a broad aspect the present invention relates to a process for reforming a gasoline fraction which comprises subjecting said fraction to contact at reforming conditions with a catalyst comprising alumina, platinum and halogen ions.

In a specific embodiment the present invention relates to a process for reforming a straight run gasoline fraction which comprises subjecting said gasoline fraction to contact at a. temperature of from about 600 to about 1000 F., a pressure of cost of the catalyst.

' sion processes has been of limited commercial acceptance because of the high cost of the catalyst. The present invention is based on the discovery that exceptionally good catalysts may be prepared to contain very low concentrations of platinum. While these catalysts may contain larger concentrations of platinum, which may range up to about by weight or more of the alumina, it has been found that exceptionally I good catalysts may be prepared to contain as low as from about 0.01% to about 1% by weight of platinum. Catalysts of these low platinum concentrations are particularly preferred in the present invention because of the considerably lower It is well known that platinum is very expensive and any satisfactory method of reducing the amount of platinum required in catalysts considerably reduces the cost of the catalyst and thus enhances the attractiveness of the catalyst for use in commercial processes. The platinum generally comprises a major portion of the cost of the catalyst and, therefore, by reducing the amount of platinum required to one half, for example, reduces the cost of the catalyst substantially by one half. Further, for example, when the amount of platinum is reduced to about 0.1% by weight as against 5% by weight, or more, as heretofore required, it is readily apparent that the cost of the catalyst is reduced by at least 50 times.

However, in order to obtain improved results with these low platinum concentrations, it is necessary that a particular type of supporting component must be composited with the platinum. It has been found that alumina shows unexpected advantages for use as a supporting component for the low platinum concentrations, apparently due to some peculiar association of the alumina with the platinum, either' as a chemical combination or merely as a physical association. It has been found that the specific combination of alumina and low platinum concentration, not only to be a very active catalyst, but also to have a long catalyst life; that is, the catalyst retains its high activity for long periods of service. After these long periods of service, the catalyst may show a drop in activity and it has further been found that the particular combination of alumina and platinum renders the catalyst susceptible to ready regeneration.

To further improve these. catalysts, it is an essential feature of the present invention that the final catalyst contains halogen ions in aspecific concentration. It has been found, and will be shown in the following examples, that the presence of halogen ions within a specific range enhances the initial activity of the catalyst and also serves to increase the life of the catalyst. It is believed that the halogen enters into some chemical combination or loose complex with the alumina and/or platinum, and thereby serves to improve the final catalyst.

While any of the halogen ions will'serve to effect improved results, the fluoride ions are particularly preferred. Next in order are the chloride ions, while the bromide and iodide ions are generally less preferred. It is understood that, while all of these halogens will serve to effect an improvement, they are not necessarily equivalent.

The catalyst of the present invention may be prepared in any suitable manner, a particularly preferred method is to prepare alumina by adding a suitable reagent, such as ammonium hydroxide, ammonium carbonate, etc. to a salt of aluminum, such as aluminum chloride, aluminum sulfate, aluminum nitrate, etc. in an amount to form aluminum hydroxide which upon drying is converted to alumina and, in the interest of simplicity, the aluminum hydroxide is referred to as alumina in the present specification and claims in order that the percentages are based on the alumina free of combined water. It has been found that aluminum chloride is generally preferred as the aluminum salt,'not only for convenience in subsequent washing and filtering procedures, but also because it appears to give best results.

After the alumina has been formed, it is generally washed to remove soluble impurities.

Usual washing procedures comprise washing with water, either in combination with filtration or as separate steps. It has been found that filtration of the alumina is improved when the wash water includes a small amount of ammoniumhydroxide. The severity of washing will depend upon the particular method employed in preparing the catalyst. In one embodiment of the invention, the alumina is thoroughly washed with a suitable amount of water and preferably water containing ammonium hydroxide to reduce the chlorine content of the alumina to below about 0.1%. In another embodiment of the invention this washing may be selective to retain chloride ions in an amount of from about 0.2% to about 5% by weight of the alumina on a dry basis. In accordance with this method of preparing the catalyst, the chloride ions are obtained from the original aluminum chloride and are retained in the alumina, thus avoiding the necessity of adding the halogen ions in a later step of catalyst preparation. However, it generally is difiicult to control the washing procedure to retain the desired amount of halogen ion and, for this reason, it usually is preferred to wash the alumina to remove substantially all of the chlorine ions and thereafter add the halogen ions in a controlled amount. The addition of the halogen ions in this manner permits better control of the amount of halogen being added. In another embodiment of the invention, the washing may be selective to retain the chloride ions in an amount constituting a portion of the total halogen desired, and the remaining portion of the halogen is then added in a subsequent step. In this method, the

I halogen ion may comprise-the same halogen or a In some cases, it may be desired to commingle an organic acid and particularly acetic acid which has been found to have a favorable effeet on the catalyst. The acetic acid apparently serves to peptize the alumina and thereby renders it "in a better condition for compositing with the platinum, and also partly to fix the platinum on the alumina so that migration of the platinum during subsequent heatin is minimized. The amount of acetic acid, when employed, will generally be within the range of from about 0.05 to about 0.5 mol of acetic'acid per mol of alumina.

want 6 v I -brown solution..,of chloroplatinic acid and my-- dream sulnde may then be commingled with [the slurry of wet alumina. gel at room tempera- ;ture; andi the slurry; sufllcie'ntly stirred to ob- Aluminajprepared in the above me washing and filtration, is gen, rallyjrecoy a wet cake. The wet cake: isusualiy made a slurry with'water' and sent to-lai for further handling. Whenthehalogen his" tain' intimate mixing'ot the "two solutions.

to be'added separately,:it preferablyjis-don h p this stage of the catalyst preparatiom-that' isg- 1 'theplatinum" is added in an; amount to produce before theplatinum is. commingledfwiththealu a viilnal 'c'a'ta'lyst containing from-about 0.01% to mina. The halogenion-mayfbe added infany {about1%"byweightofplatinum. 1

suitable manner. However; the lliitlgenjI.1 7 11591 110f In another'method ofoperation, chloroplatinic be added in a formtwhich readilyreactwith acid solutionmay be added to .the slurry of aluthe alumina-in order to- .obtainthe desiredrei 5 ".minag'el, and hydrogen sulfide then is addedto sults and also must not leave'undesireddeposlts th'emixtureg In this method of operation it has in the catalyst. A preferred me'th'odb! 'addina the-halogen is in theformfof anl acidgjsuclias hydrogen fluoride, hydrogen, emetic gen bromide ,and/or hydrogen iodide Hydr gen fluoride is 'preferablyjjadded v 5' one solution for ease in handling: and for'oon M v trol of .the specific amount to; beadded'r" and heating in the manner to be hereinother satisfactory source tO'bQ; used 'tor 1 add.-. after-[set forth. In this method, hydrogen suling the halogen is the volatileasaits such fide is not used. However, experiments have m- 1 m.v fluoride, a monium' chloride", etc. 1 shown that the hydrogen sulfide addition is prefolution with the slurry of alumina gel, and then add atroom temperature or at an elevated The l ammonium ions, will: be removed during; erable becauseit tends to further fix the platithe subsequent heating foil .twgeanm, and, mini in the .form of an insoluble compound on therefore, will v not leave undesirable deposthe a u i a o that t e p ati u comp unds itsin the catalyst.,. In still another-method, the i t grate u sthe s bs quent heat halogen may be added asfluorina' chlorine, bro-v Q h t Y Y min'e, or'iodine'but, in view of the fact that fluOr 'ha be found that best resu a obtai ed rineand-chlorine normally exist yasa gas, it. 'is"f when the platinum is composited with thealu- :of 'from about 0.2%"to' about 8%,andflprefer' a ve th u r limits v f i" a e t he lectivity of the catalyst; thus catalyzing; side v v actions to ar' lexten't g reater-jthan desiifed ,I. Afterthe alumina andihalogenphayebe vtimately. mixed, the platinui'irij maybe! a ded 'in yanyl suitabl .m r artitiu 'ar y"*preietred.-.

, I methodisltogform'aseparatesolutio "ofchloi'd "platinic' acid; in water,-.antifir tr u M 'Q sulfide intoithissolutiohf at oom mperature,

V "constant coloration ;fthat gis' ,+will notichangef color upon fthe"addition' of more hydrogen is'ulflde' generally preferable to utilize them' in the form mina'b the a u na is Subjected to substanof a solution for ease in handling. In some tial heating. As will be shown in the following cases, the inclusion of certain components; will; examples, a higher octane product was obtained notbe harmful butmaybe beneficial,- and in when the chloroplatinic acidv was added to the these cases the halogen may be Iadd'edin the wetalumina gel as compared to adding the form f of salts such as potassium fluoride, sochloroplatinic acid to alumina which had previdium fluoride, thorium' fluoride, sodium "chloride, ously been dried and formed into pills.

potassium chloride, etc. After the platinuminproper concentration has t1 lln'the preferred-embodimentof the invention' "been-found that the hydrogen sulfide may bev The concentration of halogen ion inithe finbeen commingled withthe alumina, the mixture ished catalyst will be withinrthe rangetof from 40 is. preferably dried at a temperature of from about 0.1% to. about 8% by weight of thealuabout .200 to about 400 F; tor a period of from I mine. on a dry basis. Thefluoride ion-appears about}.to24hours-ormore to form a cake. In to be more aetive and thereforefwill befusedjy"somejcases it isdesired to prepare the catalyst within the range of from about 0.1% to aboutffQinfthe form of pills of uniforni'sizeand shape, 3% by weight of the alumina on a and this may readily be'accomplished by grind- The chlorid ion will be. used withinthe-range {ing'fth partially dried catalyst cake, adding. a Q'jsuitablealubricantfsuch as "stearic acid, rosin, 1 hydrogenated coconut -oil, graphite, etc., and

ably from about 0.5% to"about-5% byftveight of the alumina' on a dry basis. It "has. been" found". that, halogen concentrations below these'lllower l m ts do t give t d si e imDi Zm n I prise'tho'seota' size ranging from about $4 x A" on thebther hand, ncent atien b fha'l en-xa. tofj%-f".fxjlq' orQthereabouts. Pills ofuniform vsizeand shape may also be formed by extrusion In fsome-cases it may be desired, to

gular sizegandshape, inwhich cases the pilling an 'e'iztrusion operations may be omitted; v

ydrogen teen of? seyeral", methods.=' Preferred method is to subject; thei catalyst to calcination at a temuntil the chloroplatinic acieniffin reaches a) te -{rename into pills in any suitable pelleting. BDDflIdtliSQ Particular satisfactory pills com- 'utllizeathecatalystas powder or granules of ir- Theeatmy timay now be" subjected to high inperature. treatment, 'and. this may comprise i l eratureofifiom -about 800 to about 1200" 1=.for- 3 a"'period.jof. from about 2 to 8hours or.more.

I a v y. o hAnother method is to subject the catalyst'to re- The chloropl'atinic acid solution is normally light tdduction with hydrogen or hydrogen-containing yeilow fla'nd, upon the addition of; hydrogen 'sul I gas at ateniperature of fromabout 300 to about fide fgas, turns tov a dark brown color; iAppafi- 000 F.I forabout 4 to 12 hours ,or more; prefer-.

entlythe chloroplatinic acid and hy'drogen'sulably followed by calcination at a temperature of fide react to-form one-or morecompl'ex chemi Q ;from about 800 to. about;1200 F. In still-ancal compounds. Best results' have been obtained other method; the' catalyst may be subjected to in this m'ethod when the hydrogen sulfide isjaddreduction with hydrogen or hydrogen-containing ed at room temperature toithe 'chloroplatinic gas at a temperature of from about 800 to about,

acid solution; The addition of hydrogen sulfide 1 1200 F. for a period of from about 2 to 10 hours at an elevated temperature of F. appears ormore.

to produce less satisfactory catalysts, The 75. In some cas es tlielubricant wili beremoved during the high temperature heating. In other cases as, for example, when graphite is used as the lubricant, the separate high temperature heating step may be omitted, and the effective heat treatment of the catalyst may be obtained in the plant before or during processing of the hydrocarbons.

Although the catalyst of the present invention will have a long life, it may be necessary to regenerate the catalyst after long periods of service. The regeneration may be effected by treatment with air or other oxygen-containing gas to burn carbonaceous deposits therefrom. In general, it is preferred to control the regeneration temperature not to exceed about 1200 F. In some cases it may be desirable to follow the burning operation with treatment with hydrogencontaining gas at temperatures of from about 700 to about 1100 F.

The reforming process will be effected at a temperature within the range of from about 600 to about 1000 F., a pressure within the range of from about 50 to about 1000 pounds per square inch and at a weight hourly space velocity of from about 0.5 to about 10. The weight hourly space velocity is defined as the weight of oil per hour per weight of catalyst in the reaction zone.

Hydrocracking reactions are favored at temperatures within the range of from about 600 to about 700 F. and at pressures within the range of from about 500 to about 1000 pounds or more. Hydrocracking is defined as cracking or splitting of carbon to carbon bonds accompanied by saturation of the fragments so formed by hydrogen present in the reaction zone and, in accordance with the present invention, the hydrocracking will be selective both in quality and in quantity as hereinbefore set forth. On the other hand the aromatization reactions are favored at temperatures within the range of from about 650 to 1000 F. and at lower pressures within the range of from about 50 pounds to about 400 pounds per square inch. It is an essential feature of the present invention that the temperature, pressure and space velocity are correlated to produce the desired aromatization and selective hydrocracking. The exact temperature, pressure and space velocity to be used in any given operation will depend upon the particular gasoline fraction being treated and the particular products desired.

In one embodiment of the process, sufilcient hydrogen will be produced in the reforming reaction to furnish the hydrogen required in the process and, therefore, it may be unnecessary to either introduce hydrogen from an extraneous source or to recycle hydrogen within the process. However, it usually will be preferred to introduce hydrogen from an extraneous source, generally at the beginning of the operation, and to recycle hydrogen within the process in order to be assured of a sufiicient hydrogen atmosphere in the reaction zone. In some cases the gas to be recycled will contain hydrogen sulfide, introduced with the charge or liberated from the catalyst, and it is within the scope of the present invention to treat the hydrogen containing gas to remove hydrogen sulfide or other impurities before recycling the hydrogen within th process.

The process of the present invention may be effected in any suitable equipment. A particularly suitable process comprises the well known fixed bed system in which the catalyst is disposed in a reaction zone and the hydrocarbons to be treated are passed therethrough in either 8 upward or downward flow. The products are fractionated to separate hydrogen and to recover the desiredproducts. As hereinbefote set forth, the hydrogen may be recycled for further use in the process. Other suitable units in which the process may be eifected include the fluidized type process in which the hydrocarbons. and catalysts are maintained in a state of turbulence. under hindered settling conditions in a reaction. zone, 1

Exsuru: I

This example shows the effect of the addition of fluoride ions to the alumina.

These catalysts wereprepared by addingammonium hydroxide to aluminum chloride hexahydrate. The resultant alumina was washed very thoroughly in order to reduce the chloride content of the alumina to below 0.1% by weight on a dry basis. This washing entailed six separate washes with large amounts of water containing a small amount of ammonium hydroxide and finally an additional wash with water. In one catalyst preparation (designated as catalyst No. 1 in the following table) hydrogen sulfide at room temperature was bubbled through an aqueous solution of chloroplatinic acid and the resultant solution was added to the alumina in an amount to produce a final catalyst containing 0.1% by weight of platinum on a dry basis. The composite was then dried for 17 hours at 572 F. and then reduced with hydrogen at 932 F. for 3 hours.

A second catalyst was prepared in substantially the same manner as described for catalyst No.

' 1, except that hydrogen fluoride was intimately mixed with the alumina before the 'chloroplatinio acid-hydrogen sulfide solution was added thereto. The hydrogen fluoride was added as a 4.8% aqueous solution and was added in an amount to produce a final catalyst containing 1.5% by weight of fluorine.

These catalysts were used for the reforming of Table 1 tl fil 0 ume e ctane Catalyst per cent of Number Charge l No Fluorine in Catalyst....- 96 I 59.8 2.. Catalyst Containingl.5%Fluorine 82.5 78.8

It will be noted that the catalyst containing fluorine yielded a reformate of 19 octane numbers higher than the catalyst containing no fluorine.

Exam lI This example shows the eifect of the addition of different amounts of fluorine to the catalyst. Catalysts No. 3 and No. 4 correspond to Catalyst No. 2 of Example I. Catalysts No. 5 and No. 6 were prepared in substantially the same manner as catalysts No. 3 and No. 4 except that the HF solution was added in an amount to produce a final catalyst containing fluorine in amounts of 3% for catalyst No. 5 and 6% for catalyst No. 6;

These catalysts were utilized for the reformin f the same gasoline described in Example I and under the same conditions of operation except that the temperature was varied as shown in the It will be noted from the above data that thetemperature and fluoride concentration, at a constant space velocity, must be correlated in order to obtain the desired results. Referring to the run with catalyst No. 3, it will be noted that the temperature is too low because the octane number of the product was only 65.7. However, when the temperature was raised to 874 F., the octane number was increased to 78.8. Using the lower temperature (824 F.) with catalyst No. 5, satisfactory results were obtained. even lowering the temperature with catalyst No. 6 containing 6% fluorine, the octane number decreased. Therefore, the maximum fluorine content of the catalyst should not exceed about 3%.

EXAMPLE HI This example shows the effect of chlorine content of the catalyst.

Catalysts No. 7, No. Band No. 9 comprised 0.1% platinum-alumina. The washing procedures were controlled to retain 0.5, 1.5 and 3.5% chlorine in the final catalyst.

These catalysts were used for the reforming of a Pennsylvania straight run naphtha having an initial boiling point of 219 F., an end boilin point of 339 F. and an A. S. T. M. motor method octane number of 41.2. These tests were conducted at a temperature of about 872 F., a pressure of about 500 pounds per square inch and a space velocity of about 2. The results of these tests are shown in the following table! It will be noted that the catalyst containing 0.5% chlorine produced a reformate of 64.2 octane number. Therefore, the chloride content of the catalyst preferably is not below about 0.5% and certainly not below about 0.2%. Catalysts No. 8 and No. 9 containing higher concentrations of chlorine produced higher octane number prod- However,

ucts. However, the chlorine content should not be increased above about 8% and preferably not above about because the catalyst will produce excessive hydro-cracking and result in an excess 5 of gas formation.

- This example shows the beneficial effects obtained in preparing the catalyst by the use of hydrogen sulfide in the manner hereinbefore set forth. Catalyst No. 10 and No. 11 were prepared in substantially the same manner except that in catalyst No. 11 the mixture of alumina and chloroplatinic acid was heated to 140 F. and hydrogen sulfide was bubbled through the mixture for 15 minutes with constant stirring. The results of these tests are indicated in the following table:

Table 4 tat-e 0....

0 6 Mm Percent of Number barge 10. Without Hydrogen 96.2 (9.8

Sulfide. n WithHydrogen but 50.1 7&4

ildo.

It will be noted that thecatalyst prepared by the addition of hydrogen sulfide gave a higher octane number product than the catalyst prepared in the absence of hydrogen sulfide.

Exnmuv This example shows the improved results obtained by adding chloroplatinic acid to wet alumina gel as compared to adding chloroplatinic acid to alumina which had been dried and formed into pills.

Catalyst No. 12 was prepared in substantially the same manner as hereinbefore set forth, while catalyst No. 13 was prepared by adding chloroplatinic acid to alumina pills which previously had been dried.

These catalysts were used for the reforming of a Mid-Continent straight run naphtha having an initial boiling point of 217 R, an end boiling point of 392 F. and an A. S. T. M. motor method octane number of 38.9. The reforming was effected at a temperature of 752 F., pressure of 200 pounds per square inch and a space velocity of 1. The results are shown in the following table: Table 5 Liquid 0cm No. Catalyst vlollglrtriie Numb;

12 Platinum added to wet alumina 92.8 68.2 13 Pla i n gm added to dry alumina 01.0 to

pills.

It will be noted that the catalyst prepared by the addition of chloroplatinic acid to wet alumina slurry produced a considerably higher octane number product under the same conditions of operation. Exmu VI This example shows the eifect of temperature of hydrogen sulfide addition in catalysts prepared by adding the hydrogen sulfide to the chloroplatinic acid solution and then adding this mix- 78 ture to the wet alumina slurry. In catalyst No.

straight run naphtha having an initial boiling point of 226 R, an end boiling point of 350 F. and an A. S. T. M. motor method octane number of 41.8. The results of these tests are shown in the following table:

Table 6 Liquid Octane No. Catal Volume m Yield Number 14 Hydrogen sulfide added at room 96.7 60.1

temperature.

16 Hydrogen sulfide added at 176 F." 07. 7 56.4

It will be noted that the catalysts prepared by adding the hydrogen sulfide at room temperature produced a somewhat higher octane number product than the catalyst prepared by adding the hydrogen sulfide at an elevated temperature.

Exmu VII Table 7 Liquid Octane No. Catalyst vgllglige Number 16 Hydrogen sulfide added at room 04.4 63.8

temperature. 17 Hydrogen sulfide added at 158 F. 95. 6 62. 8

It will be noted that the results are fairly comparable in these tests and that the effect of temperature of hydrogen sulfide treatment is not substantial in catalysts prepared by adding hy drogen sulfide to the chloroplatinic acid-alumina gel mixture.

Exsmmz VIII In view of the very low concentrations of platinum found to be efiective in catalyzing the reforming operation, the questions naturally arise as to whether such small amounts of platinum are actually of any meet and whether the platinum can not be omitted'and the same results obtained. In order to definitely show that improved results are obtained through the use of these small amounts of platinum, two catalysts were prepared in substantially the same manner except that one catalyst comprised 0.1% by weight of platinum composited with alumina, and the other catalyst comprised alumina but contained no platinum.

In a reforming operation, a Pennsylvania straight run naphtha having a boiling range of from 226 F. to 350 F. and an A. S. T. M. motor method octane number of 41.8 was subjected to conversion in the presence of the platinum-containing catalyst and in the presence of the catalyst containing no platinumat a temperature of 12 about 872' R, a pressure of 500 pounds per square inch and a weight hourly space velocity of about 2. The liquid volume yield and the A. S. T. M. motor method octane number of the products are indicated in the following table:

It will be noted that the catalyst containing no platinum yielded a product of 50.6 octane number, whereas the platinum containing catalyst yielded a product of octane number. It is readily apparent that the 0.1% by weight of platinum exerts a definite catalytic effect.

I claim as my invention:

I 1. A process for reforming a gasoline fraction which comprises subjecting said fraction to contact at reforming conditions with a catalyst comprising alumina, platinum and combined halogen.

2. The process of claim 1 further characterized in that said halogen is in an amount of from about 0.1% to about 8% by weight of said catalys 3. The process of claim 2 further characterized in that said halogen comprises fluorine in an amount of from about 0.1% to about 3 by weight of said catalyst.

4. The process of claim 1 further characterized in that said halogen comprises chlorine in an amount of from about 0.2% to about 8% by weight of said catalyst.

5. The process of claim 1 further characterized in that said platinum is in an amount of from abscut 0.01% to about 1% by weight of said catay 6. A process for reforming a saturated gasoline fraction which comprises subjecting said fraction to contact at reforming conditions with a catalyst comprising alumina, platinum in an amount of from about 0.01% to about 1% by weight of said catalyst. and combined fluorine in an amount of from about 0.1% to about 3% by weight of said catalyst.

7. A process for reforming a saturated gasoline fraction which comprises subjecting said fraction to contact at reforming conditions with a catalyst comprising alumina, platinum in an amount of from about 0.01% to about 1% by weight of said catalyst, and combined chlorine in an amount of from about 0.2% to about 8% by weight of said catalyst.

8. A process for reforming a straight run gasoline fraction which comprises subjecting said fraction to contact at a temperature of from about 600 to about 1000 F., a pressure of from about 50 to about 1000 pounds per square inch and a weight hourly space velocity of from about 0.5 to 10, in the presence of from about 0.5 to about 10 mols of hydrogen per mol of hydrocarbon, with a catalyst comprising alumina, platinum in an amount of from about 0.01% to about 1% by weight of said catalyst, and combined fluorine in an amount of from about 0.1% to about 3% by weight of said catalyst.

9. A process for reforming a straight run gasoline fraction which comprises subjecting said fraction to contact at a temperature of from about 600 to about 1000 F., a pressure of from v of from about 800 to about 1' 2oo'?"F,; I

I 13 I about 50 to about 1000 pounds per square inch and a weight hourly space velocity of from about 0.5 to 10, in the presence of from about 0.5 to

about mols of hydrogen per mol of hydrocarbon, with a catalyst comprising alumina, plati- 1% by weight of said catalyst, and combined chlorine inan amount'of from about 0.5% to about 5% byweight of said catalyst.

10. A process for reforming a gasoline fraction which comprises subjecting said fraction in con-' tact at reforming conditions, with a catalyst prepared by forming alumina from aluminum ch70- ride, washing to remove-chloride ions to below num in an amount of from about 0.1% to about about 0.1% by 'weightl'of said alumina,.com-

mingling chloride ions inana'mou'nt' of from about 0.5%. to about 5% by weight of said alumina, adding chloroplatinic acid solution in "anamount-to form a final catalyst containing which comprises subjecting said fraction tocon tact at reforming conditions with acatalyst Dre-E pared by forming a mixture ofalumina and'l'ialoe gen ions, the halogen ions said alumina on a dry basis, thereafter compositing platinum with the mixture andi subsequently heating the composite.

being in'an amount of from about 0.1% to about 8% byweight of from about 0.1% to about 1% by weight of platinum, adding hydrogen'suliideto the resultant rnixture, and'thereafterheatinglthe same at a temperature of'from about 800". to 1200? F.

v 16. A process for-reforming a gasoline fraction which comprises-subjecting saidfraction to con- ;Ctactat reforming conditions with a catalyst pre- 11. A process for reforming -a gasoline fraction which comprises subjecting said fraction to contact at reforming conditions 'witha catalyst pree pared by forming alumina from an aluminum salt,-

commingling halogen ions therewith inui an a amount of from about 0.1% to about 8% by weight of said alumina, thereafter commingling with the mixture a platinum solutionjfin an amount to form a finalcatalyst containing from r about 0.01% to about 1% by weightof platinum,

and heating the composite at a temperature of 7 .30 12. A process for reforming a gasoline. fraction from about 800 to about 120091.

j paredby'formingalumina from'aluminum emo- I ride, washing 'with'i water containing ammonium hydroxide to-r'emoyei chloride ions to belowabout 0.1%j-by weight f 'sa'idi'aluminmadding a dilute r qu o i. 1

alumina-infer;amount'to form a final catalyst "of hydrogen fluoride to said containing from. about 0.1%- to about 3% by weight, offluoride, ions based on said alumina,

separately commingling hydrogen sulfide with a I chloroplatinic acidsolutionin' an amount to form ".qannai'catalyst containingfrom about 0.01% 'to about "1 byQ-weight. of platinum, commingling the.resultant-solution with said alumina con-.

which comprises subjecting said fraction'to'con'-' T tact at reforming conditions with a catalyst prepared by forming alumina from aluminum chloride, washing to remoye chloride ions to below about 0.1%. by weight of said alumina, adding fluoride ions in an amount of from about'0.1%,

to about 3%.byweight of said alumina, separately commingling hydrogen sulfide, at f substantially room temperature with a chloroplatinic acid solu-' taining fluor ue ons, and thereafter heating the 4 resultantgcomposite at a' temperature of from about-f 800 to about "1200 F.

.17. A process for reforming a gasoline fraction 7 which comprises subjecting said fraction to contact at reforming conditions with a catalyst prepared by forming alumina from' aluminum ch oride, washing with water'containing ammonium I hydroxideto' remove chloride ions to below about tion, commingling the resultant solution at sub-' 1 stantially room temperature with said alumina containing fluorine, and thereafter heating the resultant composite at a temperature about 800 to about 1200 F.

13. A process for reforming a gasoline fraction which comprises subjecting said fraction to contact at reforming conditions with a'catalyst prepared by forming alumina from aluminum chloride, washing to remove chloride ions to below about 0.1% by weight of said alumina, adding chloride ions in an amount of from, about 0.5% to about 5% by weight of said alumina, separately commingling hydrogen sulfide 'at substantiallyv room temperature with a chloroplatinic acid solution, commingling the resultant solution at sube stantially, room temperature with said alumina containing chlorine, and thereafter heating the resultant composite at a temperature of from about 800 to about 1200 F, 1

tact at reforming conditions :with a catalyst pre- 0.1% by weight of said alumina, addingadilute aqueoussolu'tion of hydrogen chloride. to said alumina in an-amount to form a final catalyst containing from about 0.2% to about 8% by weight of chloride ions based on said alumina, separately commingling hydrogen sulfide with a chloroplatinic acid solution in an amount to form a final catalyst containing from about 0.01% to about 1% 'by'weight of-platinum, commingling the resultant solution with said alumina contain- I ing chloride'ions, and thereafter heating the resultant composite at a temperature of from about 800 to about 1200 F. j

' 18. A process for reforming a straight run gasoline fraction whichcomprises subjecting said fraction to contact at a temperature of from about 600 to about 1000 F., a pressure of from ,-'about"50-to about 1000 pounds per square inch,

and a weight'hourlyspace velocity of from about,

0.5..toabout 1'0,'inf the presence offrom about 0.5

i r I 6 14. A process for reforming a gasoline i fraction which comprises subjecting said fractionfto con'-, V

paredby forming. alumina from aluminum chloride, washing to remove chloride ions: to below about 0.1% by weight of [said alumina, com

mingling fluoride ions in an amount .offrom abou 0.l to about 3% by weight of saidf alumina,

adding chloroplatini-c, acid solution in an amount; 1

to form a final catalyst containi fi'IQm about 0.1% to about 1% by weightjofplatinum,; adding;

7 hydrogen sulfide to the resultant-mixt1ire,1andthereafter heating the same at a temperature 15. A process for reforming a gasoline hydrogen sulfide mi g rom bd amount to 5 form Q a "final {catalyst containing from about 0 .;1y%"i.to about 3%by weightfof fluoride ions bas d on s id 'l-a jum nal' Sepja 'e y; c inguns 'ith' 'a hlor'opl atinic acid solua final catalyst con-,

tion in an am with said alumina containing fluoride ions, and

thereafter heatingthe. resultant composite at a temperature of'from'ab'o'ut 800 to about 1200 1".

i to"about 1% by weight" of'platinfum, com-m hug the resultant solution 19. A process for reforming a gasoline fraction REFERENCES CITED which comprises subjecting said fraction to contact at reforming conditions with a catalyst comi fig rfiferences are of record in the prising a major proportion of alumina, from 8 n about 0.01% to about 1% by weight of platinum, 5 UNITED STATES PATENTS and from about 0.1% to about 8% by weight of Number Name 7 7 Date hamgen' VLADIMIR mam ,184,235 Groll et a1 Dec. 19, 1939 2,411,726 Holroyd et a1 Nov. 26, 1946 

